Heat Utilization in ORC Systems

ABSTRACT

Apparatus, systems and methods are provided for the improved use of waste heat recovery systems which utilize the organic Rankine cycle (ORC) to generate mechanical and/or electric power from heat sources generating power from byproducts of water purification process(es). Waste heat energy obtained from heat source(s) is provided to one or more ORC system(s) which may be operatively coupled to electric generator(s). A heat coupling subsystem provides the requisite condensation of ORC working fluid by transferring heat from ORC working fluid to one or more other process(es) or system(s), such as anaerobic digester tank(s), to provide heat energy that enhances the production of fuel for the prime mover(s) without requiring the consumption of additional energy for that purpose.

RELATED APPLICATIONS

This application is a Continuation and claims domestic benefit ofco-owned of pending U.S. Nonprovisional patent application Ser. No.14/944,213 entitled “Heat Utilization in ORC Systems” filed Nov. 18,2015, which is a Continuation-in-Part and claims domestic benefit ofco-owned pending U.S. Nonprovisional patent application Ser. No.14/625,616, now U.S. Pat. No. 9,702,271, entitled “Heat Utilization inORC Systems” filed Feb. 18, 2015, which is a Continuation of co-ownedNonprovisional patent application Ser. No. 13/758,941, now U.S. Pat. No.8,997,490, entitled “Improved Heat Utilization in ORC Systems” filedFeb. 4, 2013, which in turn claimed benefit of co-owned U.S. ProvisionalPatent Application 61/594,168 entitled “Improved Heat Utilization in ORCSystems” filed Feb. 2, 2012. All four of said applications (Ser. Nos.14/944,213, 14/625,616, 13/758,941, and 61/594,168) are incorporatedherein by reference in their entireties for all useful purposes. In theevent of inconsistency between anything stated in this specification andanything incorporated by reference in this specification, thisspecification shall govern.

FIELD OF INVENTION

The present invention relates to the apparatus, systems, and methods ofutilizing organic Rankine cycle systems for the generation of power fromwaste heat sources.

BACKGROUND

Many physical processes are inherently exothermic, meaning that someenergy previously present in another form is converted to heat by theprocess. While the generation of heat energy may be the desired outcomeof such a process, as with a boiler installed to provide radiant heat toa building using a network of conduits which circulate hot water toradiators or a furnace used for the smelting of metals, in many otherinstances unwanted heat is produced as a byproduct of the primaryprocess. One such example is that of the internal combustion engine ofan automobile where the primary function is to provide motive force butwhere the generation of significant unwanted heat is unavoidable. Evenin those processes where the generation of heat energy is desired, somedegree of residual heat unavoidably escapes or remains which can bemanaged and/or dissipated. Whether generated intentionally orincidentally, this residual, or waste, heat represents that portion ofthe input energy which was not successfully applied to the primaryfunction of the process in question. This wasted energy detracts fromthe performance, efficiency, and cost effectiveness of the system.

With respect to the internal combustion engine common to mostautomobiles, considerable waste heat energy is generated by thecombustion of fuel and the friction of moving parts within the engine.Automobiles are equipped with extensive systems that transfer the heatenergy away from the source locations and distribute that energythroughout a closed-loop recirculating system, which usually employs awater-based coolant medium flowing under pressure through jackets withinthe engine coupled to a radiator across which the imposition of forcedair dissipates a portion of the undesired heat energy into theenvironment. This cooling system is managed to permit the engine tooperate at the desired temperature, removing some but not all of theheat energy generated by the engine.

As a secondary function, a portion of the heat energy captured by theengine cooling system may be used to indirectly provide warm air asdesired to the passenger compartment for the operator's comfort. Thisrecaptured and re-tasked portion of the waste heat energy generated as abyproduct of the engine's primary function represents one familiarexample of the beneficial use of waste heat.

Very large internal combustion engines are widely used in heavy industryin numerous applications. For example, General Electric's Jenbacher gasengine division produces a full range of engines with output powercapabilities ranging from 250 kW to over 4,000 kW (by comparison, atypical mid-class automobile engine produces about 150 kW of usableoutput power). The Jenbacher engines can be powered by a variety offuels, including but not limited to natural gas, biogas (such asprovided by anaerobic digestion), and other combustible gasses includingthose from landfills, sewage, and coal mines. One common use of largecombustion engines, such as the Jenbacher model 312 and 316 engines, isto co-locate them at a biogas generation facility. This consolidates, atone location, (i) the elimination of biodegradable waste products thatrelease chemical energy in the form of combustible biogas and (ii) thecapture and combustion of the biogas in large combustion engines togenerate useful power.

These engines are frequently employed to drive electric powergenerators, converting the rotational mechanical energy from the energyof combustion into electrical energy. One such example of an anaerobicdigestion system specifically designed for the generation of electricpower from biogas is offered by Harvest Power of Waltham, Mass.

In operation, these engines generate tremendous amounts of waste heatenergy that has historically been dissipated into the environment. Inthe case of the combined Jenbacher model 316 engine and generator systemwith a maximum electric power output of approximately 835 kW,approximately 460 kW of heat energy is lost in the exhaust gas (at anapproximate temperature of 950° F.) and approximately another 570 kW islost in the cooling system (with a typical jacket water coolanttemperature of approximately 200° F.). From this data, it can be seenthat less than half of the system's power output is in the desired form(in this case, electric power output from the system generator). Unlessrecaptured and repurposed, however, the portion of the input energyconverted to heat is lost. In many prior art systems, this heat energyis lost and additional energy is required to cool the recirculatingjacket water. The heat from exhaust gas generally escapes into theatmosphere, and the recirculating jacket water is cooled by an outboardapparatus (such as by large external condensing radiators driven byforced air sources), which consume additional electric power to functionand further reduce the efficiency of the system.

Additionally, the dissipation of this waste heat energy into theenvironment can have deleterious effects. Localized heating mayadversely affect local fauna and flora and can require additional power,either generated locally or purchased commercially, to provideadditional or specialized cooling. Further, the noise generated byforced air cooling of the jacket water heat radiators can haveundesirable secondary effects.

With regard to engines fueled by anaerobic-digestion-generated biofuel,a variety of techniques, including the use of electrical heatingsystems, have been employed to provide heat energy to anaerobicdigestion processes necessary for relatively efficient generation ofbiogas by heated microorganisms. These systems consume considerableenergy and therefore have an attendant cost of operation andmaintenance. For example, the anaerobic digester heating systems offeredby Walker Process Equipment of Aurora, Ill. produce hot water in excessof 160° F. using electric power with boilers fueled by biogas, naturalgas, or fuel oil as input energy. In addition to the energy consumed toprovide this hot water, additional electric energy must be consumed tomanage the waste heat from this apparatus.

Waste heat energy systems employing the organic Rankine cycle (ORC)system have been developed and employed to recapture waste heat fromsources such as the Jenbacher 312 and 316 combustion engines. Onetypical prior art ORC system for electric power generation from wasteheat is depicted in FIG. 1. Heat exchanger 101 receives a flow of a heatexchange medium in a closed loop system heated by energy from a largeinternal combustion engine at port 106.

For example, this heat energy may be directly supplied from thecombustion engine via the jacket water heated when cooling thecombustion engine, or it may be coupled to the ORC system via anintermediate heat exchanger system installed proximate to the source ofexhaust gas of one or more combustion engines. In either event, heatedmatter from the combustion engine or heat exchanger is pumped to port106 or its dedicated equivalent. The heated matter flows through heatexchanger 101 and exits at port 107 after transferring a portion of itslatent heat energy to the separate but thermally coupled closed loop ORCsystem which typically employs an organic refrigerant as a workingfluid. Under pressure from the system pump 105, the heated workingfluid, predominantly in a gaseous state, is applied to the input port ofexpander 102, which may be a positive displacement machine of variousconfigurations, including but not limited to a twin screw expander or aturbine. Here, the heated and pressurized working fluid is allowed toexpand within the device, and such expansion produces rotational kineticenergy that is operatively coupled to drive electrical generator 103 andproduce electric power which then may be delivered to a local, isolatedpower grid or the commercial power grid. The expanded working fluid atthe output port of the expander, which typically is a mixture of liquidand gaseous working fluid, is then delivered to condenser subsystem 104where it is cooled until it has returned to a sufficiently liquid state.

The condenser subsystem sometimes includes an array of air-coolerradiators or another system of equivalent performance through which theworking fluid is circulated until it reaches the desired temperature andstate, at which point it is applied to the input of system pump 105.System pump 105 provides the motive force to pressurize the entiresystem and supply the liquid working fluid to heat exchanger 101, whereit once again is heated by the energy supplied by the combustion enginewaste heat and experiences a phase change to its gaseous state as theorganic Rankine cycle repeats. The presence of working fluid throughoutthe closed loop system ensures that the process is continuous as long assufficient heat energy is present at input port 106 to provide therequisite energy to heat the working fluid to the necessary temperature.See, for example, Langson U.S. Pat. No. 7,637,108 (“Power Compounder”)which is hereby incorporated by reference.

As a result of the transfer of waste heat energy from the combustionengine to the ORC system, these types of prior art ORC systems serve twofunctions. They convert this waste heat energy, which would otherwise belost, into productive power and they simultaneously provide abeneficial, and sometimes a necessary, cooling or condensation functionfor the combustion engine. In turn, the ORC system's shaft output powerhas been used in a variety of ways, such as to drive an electric powergenerator or to provide mechanical power to the combustion engine, apump, or some other mechanical apparatus.

ORC systems can extract as much useful heat energy as is practicablefrom one or more waste heat sources (often referred to as the “primemover”), but owing to various physical limitations they cannot convertall available waste heat to mechanical or electric power via theexpansion process discussed above. Similar in some respects to thecooling requirements of the prime mover, the ORC system requirespost-expansion cooling (condensation) of its working fluid prior torepressurization of the working fluid by the system pump and delivery ofthe working fluid to the heat exchanger. The heat energy lost in thiscondensation process, however, represents wasted energy which detractsfrom the overall efficiency of the system.

Some prior art combined prime mover/ORC engine applications haveutilized heat generated by the ORC condensation process in aconventional ORC system condenser while simultaneously providing power(electrical and/or mechanical) for various purposes. Combined heat andpower (“CHP”) ORC systems have typically fulfilled a secondary purposeby using a portion of the heat energy from the prime mover and/or heatenergy remaining in the post-expansion working fluid. FIG. 5 depicts aprior art ORC system including combustion engine heat energy output port501 and condenser heat energy output port 502.

In one prior art ORC application, residual heat extracted from adedicated ORC condenser during the cooling of post-expansion ORC workingfluid at condenser heat energy output port 502 is used to providedomestic hot water, radiant heating, or both. This process requires theuse of a conventional ORC condenser system well known in the art. Theenergy flow of such an application is depicted in the block diagram ofFIG. 6. Here, a heat generating engine 601 is operatively coupled toelectric generator 602 and provides waste heat energy 603 to the ORCsystem 604, which is operatively coupled to drive electric generator605. Heat energy from the prime mover 601 is delivered to heat energyoutput port 501 and, in some prior art systems, is extracted to (i) afirst heat energy input port 606 (such as for radiant heating) and (ii)a second heat energy input port 607 (such as for hot water heating). Inthose ORC systems known by the applicants, the utilization of residualheat from the post-expansion working fluid is intentionally extractedfrom the system but is not utilized for further system optimization ofthe prime mover or, for example, for heating a production material suchas microorganisms to generate biofuel.

BRIEF SUMMARY OF SOME ASPECTS OF DISCLOSURE

The applicants have invented apparatus, systems, and methods thatproductively utilize heat energy generated by ORC working fluidcondensation to produce fuel or other power or energy for use by theprime mover. In some embodiments, the prime mover can use the fuel,power, or energy to drive a prime mover.

In certain embodiments, the system includes: (i) a biogas generationsystem providing combustible biogas to fuel the prime mover; (ii) aprime mover that provides heat energy to drive an ORC engine; and (iii)an ORC engine that provides heat energy to drive the biogas generationsystem. In some embodiments, the biogas generation system utilizes ananaerobic digestion process which can utilize ORC heat energy tomaintain the temperature for the anaerobic process to take place.

In some embodiments, the prime mover may provide mechanical power todrive one or more electric generators. In some embodiments, suchgenerators can be connected to a power distribution grid.

In some applications, the biogas generation system can be co-locatedwith prime mover and ORC system(s) so that (i) one or more primemover(s) provide waste heat to drive one or more co-located ORCsystem(s), (ii) one or more ORC system(s) provides waste heat tomicroorganisms to drive the co-located biogas generation system, and(iii) resulting biogas can provide fuel for one or more co-located primemover(s). In some of these applications, one or more prime mover(s) andone or more ORC system(s) can simultaneously provide productive powerfor an of a wide variety of devices and applications, locally orotherwise. Alternatively or in addition, the ORC system(s) may providewaste heat to co-located heat consuming system(s) other than biogasgeneration system(s). In some applications, the prime mover may receivefuel from more than one source. For example, a prime mover may run onlocally-generated biogas during a portion of its operating schedule andanother fuel during other portions of its operating schedule. Such otherfuels may include but are not limited to stored biogas, biogas importedfrom other sources, other forms of combustible gasses, or alternatefuels (liquid, solid, or gaseous) suited to the requirements of theprime mover. In some applications, fuels from multiple sources may bemixed together and that mixture supplied to the prime mover. Thistechnique would allow the operator to control the composition of thefact and the exhaust emissions of the prime mover based in itsavailability and to maximize performance and cost efficiency of itsoperation.

In some instances, waste heat energy obtained from the exhaust gassesand/or cooling jacket water of the prime mover is provided to one ormore ORC system(s) which are operatively coupled to one or more separateelectrical generator(s) that are similarly connected to the commercialpower distribution grid. The heat coupling subsystem can comprise a heatexchanger which is operatively coupled to provide the requisitecondensation of ORC working fluid by transferring heat energy from saidfluid to one or more anaerobic digester tank(s). That heat energy canhelp optimize production of biogas from the anaerobic digestion processused to power the prime mover, and, when operated in concert with an ORCsystem also generating electric power, improve the efficiency of, andmaximize the economic benefit of, the combined system.

The prime mover of some embodiments can be any system, apparatus, orcombination of apparatus, that converts some or all of its input energyinto heat energy or waste heat energy in a form and quantity sufficientfor use by one or more ORC system(s). In some embodiments, the onlypurpose of the prime mover will be to generate heat for the ORCsystem(s). All heat energy sources co-located, compatible for use with,and utilized by one or more ORC system(s) fall within the scope of theterm “waste heat” for the purpose of this application.

In some systems, a prime mover can generate and deliver mechanical powerto an electric power generator in addition to providing waste heatenergy for the ORC system(s). In certain embodiments, a prime mover cansimultaneously generate more than one form of waste heat, including butnot limited to cooling water, hot exhaust gas, or radiated heat. Thewaste heat energy may be captured and provided to the ORC system in anypracticable manner, either directly or via one or more intermediate heatexchanger systems.

In some instances, one or more prime movers may provide waste heatenergy to one or more ORC systems. In some embodiments, a single heatexchanger may be employed for any ORC system, any prime mover, anysource of heat energy from each prime mover, or for more than one ORCsystem, prime mover, or heat energy source. These heat exchangers mayhave separate input ports and separate output ports for the energysource(s) or a single input and/or output port may be utilized for morethan one source.

In certain embodiments, one or more ORC system(s) operate with a closedloop refrigerant cycle to prevent intermixture of working fluid betweensystems. Similarly, in some instances one or more prime mover(s) operatewith a closed loop jacket water cooling system to prevent anyintermixture of jacket water between systems. In other embodiments, asingle exhaust gas heat recovery system is employed to recover wasteheat energy from more than one prime mover and provide such heat energyto more than one associated ORC system. In some embodiments, a heatrecovery system receives heat energy input from one or more sourcesand/or provides heat energy to more than one ORC system.

In some systems, one or more additional heat sources provide heat inputto the ORC system(s). For example, a portion of the biogas generated bythe anaerobic digestion process may be burned a separate boiler and usedto provide heat input to the ORC system(s) in addition to, or in lieuof, waste heat input from one or more prime mover(s).

in certain embodiments, a portion of the waste heat energy from theprime mover may be applied directly to the anaerobic digestion processwithout having been first applied to the ORC system(s). This can bebeneficial in the event that the anaerobic digestion heatingrequirements exceed the residual heat energy available from thepost-expansion working fluid in the ORC system(s).

In some applications, one or more ORC systems constitute the entirejacket water cooling system for the prime mover(s). In such cases, theORC systems may replace alternative prime mover cooling systems, whichconsume, rather than generate, power during operation and thereforeusually have a significant cost of operation in addition to their costof installation. Such power consuming dedicated prime mover coolingsystems typically have a significantly larger footprint than an ORCsystem; and therefore they may have additional physical spacerequirements at the generation facility. They may also generate noiseand unwanted environmental heat pollution as a consequence of operation.Employing one or more ORC system(s) in lieu of power consuming dedicatedprime mover cooling systems, which are net consumers of power under suchcircumstances, can be economically, physically, and environmentallybeneficial.

In some embodiments, the waste heat recovery system(s) include one ormore power generating system, which may be ORC system(s), and one ormore power receiving apparatus, which may be but are not limited toelectric power generator(s), prime mover(s), pump(s), combustionengine(s), fan(s), turbine(s), compressor(s), and the like. Therotational mechanical power generated by the power generating system(s)is delivered to the power receiving component.

In some embodiments, the ORC system(s) provide a portion of the coolingsystem for the prime mover(s) and operate in conjunction with one ormore additional cooling system(s). In some embodiments, electric powergenerated by the ORC systems may be applied to the operation of saidadditional cooling systems for the prime mover as well as provideelectric power for other purposes at the site or elsewhere. This can beparticularly advantageous if, for example, the prime mover is configuredto solely provide mechanical power output and a commercial source ofelectric power is not readily available.

In some embodiments, one or more ORC system(s) may provide heat energyto one or more anaerobic digestion tanks or other anaerobic digestionstructure. In some instances, multiple ORC systems can provide heatenergy to a single anaerobic digestion tank. In some embodiments, theanaerobic digestion heating system includes the entire condensersubsystem for the ORC system(s). In other embodiments, the anaerobicdigestion heating system comprises a portion of the ORC condensersubsystem(s) in combination with one or more other condensing system(s)which may operate on a regular or intermittent basis dictated by anumber of factors including seasonal requirements. The ambientenvironmental conditions, the number of ORC systems and their ratings,and/or the number, configuration, location, or volume of the anaerobicdigestion tanks may each be factors in determining the configuration andoperation of the condenser portion of the ORC systems.

In some embodiments, the heat energy supplied by the ORC system to theanaerobic digestion process can reduce or even completely obviate theneed for a supplemental anaerobic digestion tank heating system. In someinstances, this can reduce or even eliminate the cost of installation,maintenance, and operation of such supplemental system, including costsassociated with electric power and/or other fuels which may havepreviously been consumed by its operation. In some cases, the ORC systemcan provide heat to the anaerobic digestion process in combination withone or more other heating systems, which can serve to reduce rather thaneliminate the attendant costs.

In some embodiments, the ORC system supplies all heat required by theanaerobic digestion system via the transfer of heat energy from the ORCprocess. In some embodiments, some or all of the electric powergenerated by the ORC system can be supplied to electrical heatingsystems to heat the anaerobic digestion tank(s). This heating can be inaddition to, or in lieu of, the direct transfer of heat energy from theORC system to the anaerobic digestion system and can vary based onfactors such as the availability of heat energy and/or other electricalpower, heating requirements, and the like. In some embodiments, aportion of electric power output generated by the ORC system is suppliedto other components or systems operatively connected (eitherelectrically, mechanically, or thermally) to the combined ORC andanaerobic digestion system, including but not limited to other heatingsystems, cooling systems, fans, pumps, compressors, circulation systems,filtration equipment, stirring systems, and the like.

The foregoing is a brief summary of only some of the novel features,problem solutions, and advantages variously provided by the variousembodiments. It is to be understood that the scope of the invention isto be determined by the claims as issued and not by whether a claimaddresses an issue noted in the Background or provide a feature,solution, or advantage set forth in this Brief Summary. Further, thereare other novel features, solutions, and advantages disclosed in thisspecification; they will become apparent as this specification proceeds.

BRIEF DESCRIPTION OF THE DRAWINGS

Without limiting the invention to the features and embodiments depicted,certain aspects this disclosure, including the preferred embodiment, aredescribed in association with the appended figures in which;

FIG. 1 is a block diagram of a prior art ORC system used to convertwaste heat energy into electric power;

FIG. 2A is a block diagram of a heat coupling subsystem with heatexchangers to transfer heat energy from a closed loop system to ananaerobic digestion tank;

FIG. 2B is a block diagram of a single ORC system used to convert wasteheat energy into electric power while simultaneously providing heatenergy to a single anaerobic digestion tank that provides condensingfunctionality for the ORC system;

FIG. 2C is a block diagram of a single ORC system used to convert wasteheat energy into electric power while simultaneously providing heatenergy to a single anaerobic digestion tank that provides partialcondensing functionality for the ORC system, augmented by the presenceof a separate condenser;

FIG. 2D is a block diagram of an embodiment of this invention comprisingmultiple heat exchangers and valve(s) operative to apportion heat energythere between;

FIG. 3 is a block diagram of multiple ORC systems simultaneouslydelivering heat energy to a single anaerobic digestion tank whileproviding condensing functionality for the ORC systems;

FIG. 4 is a block diagram of a single ORC system simultaneouslydelivering heat energy to a multiple anaerobic digestion tanks whileproviding condensing functionality for the ORC system;

FIG. 5 is a block diagram of a prior art ORC system used to convertwaste heat energy into electric power including heat extraction portsthat can be used to provide heat for other applications;

FIG. 6 is a block diagram of the energy flow in a prior art systemcomprising a prime mover, an ORC system used to convert waste heatenergy into electric power, and heat extraction ports for othernon-system applications;

FIG. 7 is a block diagram of the energy flow in a system comprising aprime mover, an ORC system used to convert waste heat energy intoelectric power, and heat extraction from the prime mover used to improvesystem efficiency;

FIG. 8 is a block diagram of the energy flow in a system comprising aprime mover, an ORC system used to convert waste heat energy intoelectric power, and heat extraction from the ORC system used to improvesystem efficiency;

FIG. 9 is a block diagram of the energy flow in a system comprising aprime mover, an ORC system used to convert waste heat energy intoelectric power, and heat extraction from the prime mover and from ORCsystem used to improve system efficiency; and

FIG. 10 is a block diagram of a single ORC system used to convert wasteheat energy into electric power while simultaneously providing heatenergy to a single anaerobic digestion tank that provides condensingfunctionality for the ORC system, including heat extraction ports thatcan be used to provide heat for other applications.

DETAILED DESCRIPTION OF THE PREFERRED AND OTHER EMBODIMENTS

The process of anaerobic digestion is well known in the art. Certainstrains of bacteria, in the absence of oxygen, are employed to breakdown, or digest, certain biodegradable material including food, yard, orother waste into byproducts such as combustible gasses consisting ofmethane, hydrogen, and other trace components, as well as a residualsolid effluent byproduct. This effluent, or sludge, contains ammonia,phosphorous, potassium, and other trace materials and is beneficial toagriculture as a supplemental enrichment fertilizer for soil or as aresource suitable for combustion fuel to generate heat energy for anyuseful purpose.

The anaerobic digestion process involves three basic stages involvingdifferent microorganisms, and the temperature of the cultures can play avery significant role in the efficiency of the digestion process.Mesophilic digestion, occurring at medium temperatures, can be appliedto discrete batches of biodegradable waste while thermophilic digestion,occurring at higher temperatures, may preferably be utilized on acontinuous basis. Although the anaerobic digestion microorganisms cansurvive within the range from below freezing to above 135° F., optimaldigestion occurs at 98° F. for mesophilic organisms and 130° F. forthermophilic organisms. Bacterial activity and therefore biogasproduction is significantly reduced at greater temperatures and declinesat a somewhat lesser rate at cooler temperatures. The requirement forheating of the cultures may vary over time (over the course of a singleday and, as seasons change, throughout the year) based on ambienttemperatures.

With reference now to FIG. 2A, a heat coupling subsystem 201 can be usedto transfer heat energy to the anaerobic digestion process whilemaintaining media isolation between a heat source and an anaerobicdigestion system in the heating tank 208, owing to potentially differentmedia requirements of the two systems. The heat coupling subsystem 201includes (i) an intermediate heat exchanger 204, (ii) an anaerobicdigestion tank heat exchanger 207 within, as part of the wall of, orotherwise in direct thermal communication with, the anaerobic digestiontank 208, (iv) pumping apparatus 209 between the tank heat exchanger 207and the intermediate heat exchanger 204, (v) operative coupling betweenthe various components described below, and (vi) secondary media (whichmay be the same as or different from the primary medium depending onsystem requirements) flowing within the isolated closed loop provided bythe tank-side (secondary) portion of the heat coupling subsystem 201 viathe input port 206 and the output port 205, the anaerobic digestion tankheat exchanger 207, and the pumping apparatus 209. Heat couplingsubsystem 201 may also include storage reservoirs (not shown) for aquantity of both the primary medium and the secondary medium asnecessary to insure that sufficient media is available for the properoperation of each closed loop systems on the primary and secondarysides.

The primary side of the intermediate heat exchanger 204 includes aprimary side input port 202 to receive the heated primary media (notshown) from the heat source, which may be an ORC system, a prime mover,or any other source of heat energy, a primary side heat exchangersection 204A, and a primary side output port 203. This flow providesheat energy from the ORC system for transfer to, and use by, theanaerobic digestion tank(s), e.g., 208. The heated primary media can beORC working fluid, water, a mixture of water and ethyl glycol, a mixtureof water and one or more other components, or any other fluid or gaseoussubstance compatible with the application and apparatus. The heatedprimary media passes through the primary side 204A of intermediate heatexchanger 204 and exits at primary side exit port 203. Heat energy fromthe heated primary media is transferred to the secondary side of theintermediate heat exchanger 204, through which a suitable secondarymedia (not shown) enters at secondary side input port 206, flows throughsecondary side heat exchanger section 204B, and exits at secondary sideoutput port 205. This heated secondary media then flows throughanaerobic digestion tank heat exchanger 207, where heat energy istransferred from the heated secondary media to the contents of anaerobicdigestion tank 208 before being pressurized by pumping apparatus 209 andreturned to secondary side of the intermediate heat exchanger 204 at thesecondary side input port 206.

With reference now to FIG. 2B, an ORC system, generally 200, utilizesthe heat coupling subsystem 201 within, as part of the wall of, orotherwise in direct thermal communication within anaerobic digestiontank 208 to provide cooling for the post-expansion working fluid exitingfrom the expander 102. The ORC working fluid exits the expander 102 andenters input port 202, travels through the heat coupling subsystem 201,and then exits the output port 203 and enters the system pump 105. Theheat coupling subsystem 201 and anaerobic digestion tank 208 thereforeprovide an integrated working fluid condensation and heat consumptionsystem. That is, the anaerobic digestion tank heat exchanger 207, whencoupled to the ORC system via intermediate heat exchanger 204 in themanner shown in FIG. 2A and described in detail above, comprise heatcoupling subsystem 201 which may be considered to function as a singleheat exchanger for the purposes of the ORC system. Analogous to theperformance of a transformer in an electrical system, heat couplingsubsystem 201 serves as a “thermal transformer” which transfers heatenergy from its primary (ORC) side to its secondary (tank) side whilemaintaining isolation between the separate media flowing in each closedloop. This provides the equivalent performance of a condenser known inthe prior art with significant improvements. This particular system isalso a production system, meaning that the heat coupling subsystem 201provides heat energy, via anaerobic digestion tank heat exchanger 207,directly for production and not for mere disposition of the heat aswaste. In this example, the anaerobic digestion tank heat exchanger 207directly heats the contents of the anaerobic digestion tank 208,yielding production of biogas. The temperature of the post-expansionworking fluid entering input port 202 should be about 125° F., which isnearly ideal for the purpose of supplying heat to a continuousmesophilic anaerobic digestion process including the heat energy lossesfrom an intervening intermediate heat exchanger.

Referring to both FIGS. 2A and 2B, in an embodiment utilizing anintermediate heat exchanger 204, less heat energy will be delivered tothe anaerobic digestion tank(s) than is provided to the primary side,i.e., through input port 202, of heat coupling subsystem 201 due to theunavoidable loss of heat energy during the heat transfer process fromthe primary medium to the secondary medium via intermediate heatexchanger 204. However, for applications with reduced anaerobicdigestion heating requirements, such as mesophilic digestion processes,this loss of heat energy can be beneficial and can eliminate therequirement for a dedicated supplemental condensing apparatus. Thismethod may be applied to any configuration of the anaerobic digestionheating apparatus.

With reference now to FIG. 2C, the structure and operation of the systemis identical to that of FIG. 2B with the addition of an ORC condensersubsystem 104 between the input port 202 and the outlet port 203.Condenser subsystem 104 functions as a heat exchanger removing energyfrom the post-expansion working fluid to restore the working fluid to asufficiently liquid state. The energy removed from the working fluid, inthe form of heat, is transferred to an alternate medium, such as air ora liquid, for removal from the ORC system. In this embodiment comprisingboth heat coupling subsystem 201 and condenser subsystem 104,post-expansion ORC working fluid can thus travel through either or both(i) the condenser subsystem 104 and (ii) the heat coupling subsystem 201associated with the anaerobic digestion tank 208. This embodiment may beused when insufficient condensing capacity might be provided by theanaerobic digestion tank 208 or during periods of ORC operation when theanaerobic digestion tank 208 is not in service. This embodiment permitsthe flow of post-expansion working fluid directly from the outlet port203 of the expander 102 directly to either condenser subsystem 104 orthrough heat coupling subsystem 201. This will generally provide thegreatest temperature working fluid to heat coupling subsystem 201 andwill permit complete disassociation of heat coupling subsystem 201 fromORC operation via the use of appropriate valves (not shown) at thejunctions of heat coupling subsystem 201 and the inlet and outlet ofcondenser subsystem 104. Condenser subsystem 104 may generally be anytype of condenser system best suited for the particular application andfactors that govern the installation and operation of the ORC system,including but not limited to the mass flow rate of working fluid in theORC system, ambient temperature conditions including both diurnal andseasonal variations, equipment footprint, installation and maintenancecost, and the like. In one embodiment, condenser subsystem 104 maycomprise one or more air cooled radiators with forced air, as themedium, being driven through the radiator(s) by one or more fans. In oneembodiment, condenser subsystem 104 may comprise one or more radiatorswherein a flow of a liquid medium is in heat transfer communication withthe post-expansion working fluid. In both embodiments, the media iseither discharged from the system or circulated and adequately cooled ina separate system. All other configurations of condensing subsystemsknown in the art and applicable to ORC systems are also envisioned bythis disclosure.

In a related embodiment shown in FIG. 2D, a condensing transfer system220 comprises an intermediate heat transfer unit 104A, condensingsubsystem pump 221, one or more valve(s) 222, anaerobic digester heatexchanger 223, and one or more secondary heat exchanger(s) 228, all inheat energy transfer communication via a separate condenser heattransfer medium flowing between said elements. Post-expansion workingfluid is conveyed to condensing transfer system 220 via intermediateheat transfer unit 104A through which the separate condenser heattransfer medium, in heat transfer receiving communication with theworking fluid, is circulated via motive force provided by condensingsubsystem pump 221. Said medium is separate from the ORC working fluidand may comprise water, oil, an organic refrigerant, an inorganiccompound, or any other fluid or combinations of fluids of suitableperformance to accept heat energy from the working fluid and providesaid heat energy to one or more condensing subsystems comprising theremainder of condensing transfer system 220. Heat energy is transferredfrom the post-expansion working fluid to the condenser heat transfermedium in intermediate heat transfer unit 104A, thereby heating thecondenser heat transfer medium and restoring the post-expansion workingfluid to a sufficiently liquid state suitable for pressurization bysystem pump 105 for reheating and subsequent expansion in the ORC systemas described elsewhere herein.

Condensing subsystem pump 221 provides pressurization of the heatedcondenser heat transfer medium necessary to convey said heated medium toheat exchangers 223, 228, and others similarly connected via the one ormore valve(s) 222 that permit the flow of heated condenser heat transfermedium to be controllably distributed in any desired proportion asnecessary and desirable for system optimization. One or more valve(s)222 are configured receive the condenser heat transfer medium from pump221 and direct all of said heated condenser heat transfer medium to anyone of said heat exchangers, direct any portion of said heated condenserheat transfer medium to any one heat exchanger and any other portion(s)to any other heat exchanger(s), or to direct no heated condenser heattransfer medium to any one or more than one of the heat exchangers.However, as described below, at least a portion of heated condenser heattransfer medium must be directed to at least one heat exchanger. In thismanner, the most efficient and effective use of the heat energy removedfrom the post-expansion working fluid may be realized.

FIG. 2D depicts anaerobic digester heat exchanger 223 in heatedcondenser heat transfer medium receiving communication with valve(s)222. In one embodiment, anaerobic digester heat exchanger 223 may beintermediate heat exchanger 201 disclosed elsewhere herein and depictedin FIG. 2A as being a component of heat coupling subsystem 201. In thisembodiment, primary side input port 202 and primary side output port 203of intermediate heat exchanger 201 correspond to primary side input port224 and primary side output port 226, respectively, of anaerobicdigester heat exchanger 223. Further, secondary side input port 206 andsecondary side output port 205 of intermediate heat exchanger 201correspond to secondary side input port 227 and secondary side outputport 225 of anaerobic digester heat exchanger 223. The primary andsecondary sides of anaerobic digester heat exchanger 223 are in thermaltransfer communication, allowing heat energy to be transferred from theheated condenser heat transfer medium in the primary side to a separatemedium flowing in the secondary side. Said separate medium may comprisewater, oil, an organic refrigerant, an inorganic compound, or any otherfluid or combination of fluids of suitable performance. The remainingcomponents of intermediate heat exchanger 201 may be identicallyconfigured as described and depicted in FIG. 2A in this embodiment.

In one embodiment, anaerobic digester heat exchanger 223 may beconfigured to provide heat energy to an anaerobic digestion tank in anyother manner described herein or otherwise known in the art. By way ofexample and not limitation, anaerobic digester heat exchanger 223 may beused in conjunction with the embodiments depicted herein as FIG. 3, 4,8, 9 or 10.

FIG. 2D also depicts secondary heat exchanger(s) 228 in heated condenserheat transfer medium receiving communication with valve(s) 222. Here,primary side input port 229 receives a flow of heated condenser heattransfer medium from valve(s) 222 which passes through the primary sideof secondary heat exchanger(s) 228 and exits at output port 231. Anadditional and separate heat transfer medium, which may comprise water,oil, an organic refrigerant, an inorganic compound, or any other fluidor combination of fluids of suitable performance, enters the secondaryside of secondary heat exchanger(s) 228 at input port 232, passesthrough the secondary side of secondary heat exchanger(s) 228, and exitsat output port 230. The primary and secondary sides of secondary heatexchanger(s) 228 are in thermal transfer communication, thereby allowingheat energy to be transferred from the heated condenser heat transfermedium in the primary side to the separate medium flowing in thesecondary side. In this manner, heat energy from the heated condenserheat transfer medium is transferred to the separate medium and therebyremoved from condensing transfer system 220.

Although only one exemplary secondary heat exchanger 228 is depicted inFIG. 2D for clarity, it should be understood that the instant disclosureprovides for more than one such heat exchanger in a similar orfunctionally equivalent arrangement (not shown). Additional valve(s) 222may be utilized to provide a controllable portion, ranging from none toall, of the heated condenser heat transfer medium from said valves toany of one or more heat exchanger(s) 228 deemed necessary or desirableto provide sufficient cooling for the ORC system and to provide andutilize heat for any other desired purpose known in the art or laterdeveloped.

In one embodiment, secondary heat exchanger(s) 228 comprise one or moreair cooled radiators subjected to forced air cooling provided byelectric fans. In this manner, heat energy from the heated condenserheat transfer medium is transferred to the forced air flow and therebyremoved from condensing transfer system 220. Said electric fans may bepowered by electric power from a commercial power grid, by electricpower provided by one or more generator(s) driven by mechanical powerderived from the ORC expander(s), by electric power provided by anotherlocal generator associated with the prime mover(s) or anaerobicdigestion system, by mechanical power provided directly or indirectly bya rotating shaft in or associated with one or more ORC expander(s), bymechanical power provided directly or indirectly by another rotatingshaft in or associated with the prime mover(s) or anaerobic digestionsystem, or by any other preferred source of electric or mechanicalpower.

In one embodiment, secondary heat exchanger(s) 228 comprise one or moreliquid cooled radiators through which a flow of cooling liquid,including but not limited to water, is passed through the secondary sidein heat energy receiving communication with the heated condenser heattransfer medium flowing in the primary side such that heat energy fromthe heated condenser heat transfer medium is transferred to coolingliquid and thereby removed from condensing transfer system 220. In oneembodiment, the cooling liquid may be cooled via any preferred means andre-circulated back to the secondary side of secondary heat exchanger(s)228 in a closed-loop circuit. In an alternative embodiment, andpreferably when the cooling liquid is water, when a large supply ofwater is available, and when the discharge of water heated by thecondenser heat transfer medium is both feasible and preferred, noattempt is made to intentionally cool and re-circulate the coolingwater. For example, cooling water may be extracted from a source suchas, but not limited to, a well, a pond, or a large reservoir, providedto secondary heat exchanger(s) 228 for cooling purposes, and thendischarged back into the same source or a different source. In oneembodiment, such cooling water may be extracted at or near a cool pointof the source and, after passing through secondary heat exchanger(s)228, be discharged at or near a warm point. In warm summer months, thecoolest point may be at the greatest depth of the source and the warmestpoint may be at the surface. In cold winter months, the upper surface ofthe source may be at or near freezing temperatures while the warmestpoint may be at the greatest depth. In the latter case, even the warmesttemperature will likely be sufficient for use by secondary heatexchanger(s) 228, and discharging water warmed by the heat transferprocess at the surface may be preferred to prevent the source fromfreezing. Any preferred combinations of water extraction and return areobvious to a person of ordinary skill in the art and are thereforeenvisioned by this disclosure. In this manner, the temperaturecharacteristics of the source of cooling water may be controlled to somedegree, although such control is a potential advantage secondary to thatof the energy conversion and creation advantages described elsewhereherein. Although extracting and returning the water to and from,respectively, the same source allows for some or all of the same waterto be used more than once, the open nature of this arrangement isdistinguishable from the recirculating closed loop embodiment describedabove because new (additional) water may be added and previously-usedwater may be removed from the system at any time, including viaevaporation, unlike in a typical closed loop system where a finitequantity of water is re-circulated without addition or subtraction inthe normal course of operation. In one embodiment, water obtained forcooling from one source may be returned to a different source wheneverbeneficial for any other secondary purpose.

With reference now to FIG. 3, a series of ORC systems 301, 302, 303 arecombined to provide heat energy to an anaerobic digestion tank 308.Although three ORC systems are depicted, any number of ORC systems canbe included to provide the desired level of heat transfer to theanaerobic digestion tank 308. This embodiment may be particularlyadvantageous for large anaerobic digestion facilities in order tomaintain a uniform temperature throughout a large volume anaerobicdigestion tank 308. Since the temperature of the medium circulatingwithin the anaerobic digestion heating system can be higher at its pointof entry into the tank and generally lowest at its point of exit as theheat energy is transferred to the contents of the tank, the introductionof several independent ORC systems, e.g., 301, 302, 303 at differentlocations in the anaerobic tank 308 can provide for a more evendistribution of heat and corresponding uniform temperature than would bepossible from a single source.

The same or similar result may be achieved by a single ORC system (notshown) using a specially designed manifold system (not shown) havingmultiple heat coupling subsystems 201. For larger digestion tanks,however, the finite heat energy available from a single ORC system maybe insufficient to maintain the temperature of the tank contentsuniformly at its desired, and in some instances, optimal value. Anyconfiguration of heat coupling subsystems 201 may be employed to provideoptimal results.

In order to provide the desired results, the geometry and configurationof an anaerobic digestion tank heat exchanger 201 used to simultaneouslyheat the contents of the anaerobic digestion tank(s) and providecondensation of the post-expansion working fluid can be designed andimplemented in view of the desired performance of both subsystems. Inone embodiment, the heated medium (the post-expansion working fluid)flowing within the anaerobic digestion tank heat exchanger 201 maydirectly circulate within a series of interconnected pipes and/ormanifolds (not shown) inside the anaerobic digestion tank(s). Thesestructures can be essentially planar with media flows in a single plane(neglecting the thickness of the components) or may be more threedimensional with heated medium flows in two or more planes. Theconfiguration of the anaerobic digestion tank heat exchanger 201 may bedesigned with, as shown in FIGS. 2B and 2C, a single input port 202 andoutput port 203 or may be configured with, as shown in FIG. 3, multipleinput ports 202 and output ports 203 to provide a more uniformdistribution of heat throughout the anaerobic digestion tank 308.Further, the interconnected pipes and/or manifolds may include a seriesof valves that permit control and redirection of the heated medium tovarious regions of the anaerobic digestion tank 308 as may be desired toachieve the preferred distribution of heat. In another embodiment, theheated medium may circulate through sealed channels embedded in thewalls of the anaerobic digestion tank(s), thereby heating the contentsof the tank at its interior boundaries or side wall(s).

With reference now to FIG. 4, a single ORC system 400 may be used toprovide heat energy to more than one anaerobic digestion tank (notshown) via multiple heat coupling subsystems 401, 402, and 403. In thisembodiment, the available heat energy from post-expansion working fluidfrom an ORC system 400 is distributed to anaerobic digestion tank heatexchangers (not shown) in each of three discrete anaerobic digestiontanks (not shown) via heat coupling subsystems 401, 402, and 403. Eachof these heat coupling subsystems 401, 402, 403 may be comparable toheat coupling subsystem 201 shown in FIG. 2A. The specific distributionof post-expansion working fluid provided to each heat coupling subsystem401, 402, 403 can be controlled, varying it as needed to allocate theavailable heat energy among the several tanks. In some instances, thismethod can be well suited for smaller tanks, systems with reducedrequirements for anaerobic digestion heating, or lower temperaturemesophilic batch processing, particularly where not all tanks are insimultaneous use. Although three tanks are referenced here, any numberof tanks are envisioned that provide the requisite performance.

These combined ORC and anaerobic digestion systems are distinguishedfrom known prior combined heat and power systems in that the priortechnology merely siphons some portion of heat energy from ports addedto known ORC systems. The known prior art does not teach, for example,the replacement of ORC condenser systems, in whole or in part, with analternate system including one that simultaneously provides, via oneheat coupling subsystem: (i) heating directly to a heat consumingprocess which provides some beneficial function and (ii) an equivalentcooling and condensation function for the ORC working fluid primarymedia, which may be heated post-expansion working fluid from the ORC. Inthis regard, known prior art ORC systems typically require significantelectric power to drive fans or an equivalent cooling system. Theeconomic advantage of generating power from waste heat energy is greatlyreduced when a large portion of the generated power is consumed by thesystem's internal requirements (sometimes referred to as the “parasiticload”). The combined ORC and anaerobic digestion system thus provides adouble economic advantage; not only is the requisite cooling providedfor the primary media, which in the case of an ORC will be heatedpost-expansion working fluid, without additional electric powerconsumption, but the electric power normally required to maintain theanaerobic digestion tanks at the optimal temperature is no longerrequired due to the transfer of heat energy from the companion ORCsystem. While the known prior art requires electric power tosimultaneously cool the ORC media and heat the anaerobic digestiontanks, the combined ORC and anaerobic digestion system reduces oreliminates both requirements for electric power by transferring unwantedheat energy directly via heat coupling subsystem 201 from the ORC systemto the anaerobic digestion system. As a result, the net electric powergenerated by the combined ORC and anaerobic digestion system issignificantly greater than in the present art, providing greatereconomic benefit while conserving resources necessary to produceelectric power.

In some embodiments of the present application, anaerobicdigestion-based biogas power generation systems can be enhanced byintegrating the functions of an ORC waste heat energy generation systemwith the biogas-burning prime mover and the anaerobic digestion processwhich generates the biogas for the prime mover. Both the heat input andheat output of the ORC system can be coupled to other components withinthe overall system. Unlike the known prior art, which does not integrateall three subsystems into a single optimized energy conversion system,some embodiments of the present application provide for increased andpossibly maximum efficiency by utilizing more and possibly all availableheat energy within the system to a greater, and possibly the greatest,extent practicable.

In certain embodiments, no heat energy is intentionally dissipated orredirected to any non-system application. In certain instances, as someor all of the lowest grade residual waste heat energy remaining aftertwo stages of electric power generation is returned to enhance, and insome instances optimize, the production of fuel for the primary electricpower generation process, the system forms a novel and more effectivethree stage closed-energy-loop.

More specifically, the novel combined prime mover, ORC, and anaerobicdigestion system taught herein uniquely allows for each of the threecomponent systems to provide operational benefits of the other two.Specifically, the anaerobic digestion system can, in certainembodiments, be the anaerobic digestion system offered by Harvest Poweras described above. In certain embodiments, the prime mover(s), whichcan be the Jenbacher 312 or 316 internal combustion engines alsodescribed above, are fueled by biogas produced by the anaerobicdigestion process and cooled, in whole or in part, by one or more ORCsystem(s) which remove undesired waste heat energy and convert it touseful mechanical and/or electrical power. In this manner, the ORCsystem(s), which in certain embodiments can be Power+™ ORC system(s)offered by ElectraTherm, Inc. of Reno, Nev., receive their input energyin the form of waste heat from the prime mover(s) and providepost-expansion heat energy to the anaerobic digestion process to enhancethe production of biogas fuel for the prime mover(s). Additionally, theheat energy from the ORC that is absorbed by the anaerobic digestionprocess system provides the necessary cooling condensation ofpost-expansion ORC working fluid, obviating the need for a separate ORCcondenser and the attendant cost of operation. As each of the threecomponent system enhance the operation of the other two, all availableheat energy is utilized to the greatest extent possible and the need foradditional energy, particularly electrical energy, to provide coolingand/or heating as in the present art is minimized or eliminated.

In one embodiment depicted in FIG. 7, the prime mover 601 cansimultaneously contribute heat energy and/or waste heat energy 603 tothe ORC system 604 and heat energy 702 to the anaerobic digestion tank701, which provides the biogas fuel for the prime mover 601.

In an embodiment depicted in FIG. 8, the ORC system 604 can obtain itsheat input from the waste heat energy 603 of prime mover 601 and deliverits own waste heat energy 801 to the anaerobic digestion process. Heatenergy flow 801 may be provided from the post-expansion working fluid toanaerobic digestion tank 701.

In an embodiments depicted in FIG. 9, both the prime mover 601 and theORC system 604 provide heat energy to anaerobic digestion tank 701 asdepicted in FIG. 9 via heat flows 702 and 801, respectively.

In addition to the heat energy being transferred from the primary media(which in some embodiments may be post-expansion ORC working fluid) tothe anaerobic digestion process to increase the efficiency of theoverall system, heat energy may also be extracted for other purposes.With reference now to FIG. 10, a prime mover (not shown in FIG. 10) canprovide heated prime mover media to the heat exchanger 101 of an ORCsystem 1000 and to a prime mover heat energy output port 501.Post-expansion working fluid heat energy can be provided to theanaerobic digestion tank heat exchanger 201 and to an output port 1001;and post-anaerobic digestion tank heat exchanger heat energy can beprovided to output port 1002. Any combination of these ports may beutilized to provide heat energy for one or more purposes not related tothe operation of the CHP system.

One or more embodiments of this invention are particularly well-suitedfor use in wastewater treatment systems where anaerobic digestionsystems are common and excess biogas produced by said digestion systemsis often burned as flares simply for disposal purposes without providingany beneficial use or other advantage. For the purposes of thisdisclosure, the phrase “wastewater treatment” shall refer to any or allof the individual processes known in the art whereby chemical,biological, or any other contaminates are removed from an aqueoussolution so as to reduce the level of said contaminants, particularlybut not necessarily to a level wherein said aqueous solution is suitablefor human consumption or unrestricted use. Examples of wastewatertreatment facilities include, but are not limited to, sewage treatmentplants, irrigation water reclamation processing facilities, and thelike. In one wastewater treatment embodiment, the prime mover providingheat to the ORC system may be an internal combustion engine fueled atleast in part by the biogas generated as a byproduct of the anaerobicdigestion system as disclosed elsewhere herein. Heat energy from theengine jacket cooling water or exhaust gas may be utilized by the ORC.In one embodiment, input heat energy for the ORC system may be providedby one or more boilers fueled by the biogas generated by the anaerobicdigestion system or other co-located process as disclosed elsewhereherein. Whenever the term is used anywhere within the scope or appliesto any understanding of this disclosure, a co-located device, system orprocess is one at or sufficiently proximate to the system disclosedherein such that any input or output of said device, system or processmay be communicated to any input or output of any device, system orprocesses directly or indirectly associated with the disclosed system.Means of such communication between devices, systems, or processes maybe via any useful means, including but not limited to wires, cable,conductors, electromagnetic waves, pipes, tubing, conduit, raceways,rigid or flexible mechanical devices such as rods, shafts, or linkagesof any kind, heat energy radiation, heat energy conduction, or by anyother known or subsequently developed means. In one embodiment, inputheat energy for the ORC system may be provided by any combination ofinternal combustion engines or boilers. In one embodiment, input heatfor the ORC system may be provided by one or more fuel cells ormicroturbines. In one embodiment, the dry sludge biosolid byproducts ofthe anaerobic digestion process or any other co-located process may alsobe incinerated in one or more boiler(s) and the heat energy of saidincineration supplied to the input of the ORC system.

In one non-limiting exemplary embodiment pertinent to wastewatertreatment, heat energy may be delivered to system input port 106 of FIG.2D at an approximate temperature of 240° F. from one or more sources ofheat comprising at least one of any of boiler(s) or internal combustionengine(s) consuming some or all of the biogas generated by the localanaerobic digestion system or by any other co-located system or process.The ORC system operates as described elsewhere herein, generatingmechanical power via the expansion of heated working fluid in expander102 and either conveying that mechanical power to generator 103 toprovide electrical power output or using the mechanical power directlyfor some other beneficial purpose.

ORC condensing transfer system 220 is provided to remove residualunwanted heat energy from the post-expansion ORC working fluid andthereby return said working fluid to a sufficiently liquid state. Atinlet 233 of intermediate heat transfer unit 104A, condenser heattransfer medium is provided at an approximate temperature of 55°-75° F.at a flow rate of approximately 200 gallons per minute. After receivingheat energy transferred by the post-expansion working fluid, condenserheat transfer medium, now heated to an approximate temperature of110°-113° F., exits intermediate heat transfer unit 104A at outlet 234and is pressurized by condensing subsystem pump 221 and conveyed to oneor more valve(s) 222.

In one mode of operation of this embodiment, at least a portion of theheated condenser heat transfer medium is provided from said one or morevalve(s) 222 to anaerobic digester heat exchanger 223 via input port224. Here, heat energy is transferred from the heated condenser heattransfer medium to the anaerobic digestion system to maintain thetemperature of the cultures in the range of 100°-103° F. for certaincultures and generally within a broader range of 95°-105° suitable formost mesophilic organisms. It should be appreciated the quantity of heatenergy available from the system, the temperature of the heatedcondenser heat transfer medium applied to intermediate heat transferunit 104A, the volume of the anaerobic digestion tanks, the ambienttemperature, and a myriad of other factors will require some degree ofregulation in the amount of heat energy necessary to maintain thecultures at their optimum temperature. Such regulation may be providedby the one or more valve(s) 222 via regulation of the mass flow rate ofheated condenser heat transfer medium flowing there through. Preferably,the anaerobic digestion tank(s) and condensing transfer system 220disclosed in detail below each comprise one or more temperature sensorsdisposed at advantageous points in the system so that the one or morevalve(s) 222 may be continuously configured to maintain the temperatureof the cultures as desired. When heat energy is required by thecultures, said one or more valve(s) 222 may be operative to provide therequisite heat energy via an increased flow of heated condenser heattransfer medium to anaerobic digester heat exchanger 223. Whenadditional heat energy is no longer required by the cultures, the one ormore valve(s) 222 may be operative to reduce or discontinue the flow ofheated condenser heat transfer medium to anaerobic digester heatexchanger 223.

It is important to appreciate that under many circumstances, the heatrequirements of anaerobic cultures is wholly independent of the coolingrequirements of the ORC system and that the system must be configurableto adequately, and preferably optimally, ensure both requirements aresimultaneously achieved at all times. Under certain conditions, the ORCsystem may require additional cooling while the anaerobic digestionsystem requires additional heat energy; these simultaneous requirementsare complementary since the additional heat extracted from the ORCsystem would be available to the anaerobic digestion system. However,conditions such as high ambient temperature will generally requireadditional ORC cooling while also reducing the amount of heat requiredby the cultures, and these simultaneous requirements are contradictoryrather than complementary. Excess heat extracted via the ORC coolingprocess may not be transferred to the cultures without exceeding theiroptimal temperature, but it must still be extracted from the ORC systemto provide proper working fluid condensation and then dissipated orconsumed elsewhere.

Accordingly, in another mode of operation, the one or more valve(s) 222are operative to reduce or discontinue the flow of heated condenser heattransfer medium to anaerobic digester heat exchanger 223 whilesimultaneously increasing the flow of heated condenser heat transfermedium to the one or more secondary heat exchanger(s) 228. In thismanner, the one or more secondary heat exchanger(s) 228 provide a safetyvalve of sorts for the ORC system which cannot operate without adequatecooling and condensation of the post-expansion working fluid.Preferably, the ORC system, the anaerobic digestion system, and theassociated condensing transfer system 220 which operatively connects thetwo will be provided with sufficient operational flexibility to provideheat energy to the anaerobic digestion cultures under all reasonableconditions and sufficient capacity to provide working fluidcondensation/cooling to the ORC system under all reasonable conditions.To accomplish this purpose, the ORC system will also preferably compriseone or more temperature sensors disposed at advantageous points in thesystem so that the one or more valve(s) 222 may be continuouslyconfigured to provide the necessary ORC cooling as desired.

In this and other embodiments, the one or more secondary heatexchanger(s) 228 may comprise any configuration disclosed above, anyknown otherwise in the art, or any that may be later developed. However,the presence of large reservoirs of treated effluent at wastewatertreatment plants enable the preferred use of liquid-cooled radiatorsdescribed above. At such facilities, the temperature of the on-sitetreated effluent is not typically regulated or maintained within anyspecific range, and given the massive aggregate volume of availabletreated effluent and the relatively low mass flow rate required toprovide ORC cooling, the heat energy of any portion of, or all portionsof, the heated condenser heat transfer medium may be easily consumed bysaid treated effluent with only incidental incremental cost and withminimal change in temperature to the aggregate volume thereof. In lieuof massive air-cooled radiators driven by large fans consuming electricpower, one or more compact and relatively inexpensive liquid-cooledradiators may be provided. Such radiators, broadly described as heatexchangers, transfer heat energy from the ORC working fluid to anexternal sink directly or via intermediate means. Specifically, in oneembodiment, a flow of heated condenser heat transfer medium in theprimary side of a standard heat exchanger functioning as a radiator maybe provided in heat energy transfer communication with treated effluentfrom the wastewater facility counterflowing in the secondary side, wheresaid effluent may provide up to all of the cooling capacity required bythe ORC system, even during periods when such cooling requirements aremaximized while heat consumption by the anaerobic digestion system isminimized. Further, said effluent may be obtained and discharged intothe same reservoirs without the need for a closed loop circulationsystem with active cooling known in the present art. Generally, sucheffluent is available for use by the one or more secondary heatexchanger(s) 228 within the range of 50°-70° F., sufficient to cool theheated condenser heat transfer medium to the specified range of 55°-75°F. for application to inlet 233 of intermediate heat transfer unit 104A.Generally, a treated effluent flow of 250-350 gallons per minute will berequired for an ORC system configured to generate a net electric poweroutput of 75-92 kWe, which is optimal for the Power+™ ORC system(s)offered by ElectraTherm, Inc. In other embodiments, any otherconfiguration of heat exchanger may be utilized to remove heat from theheated condenser heat transfer medium. For example, a series ofmanifolds or ducting may be disposed within reservoirs of treatedeffluent or other media of an appropriate temperature and the heatedcondenser heat transfer medium cooled by passage through said manifoldsor ducting in thermal transfer communication with the treated effluentor other media without the need to establish an active flow of coolingmedia through a particular apparatus.

In one embodiment, the heat consumed from the post-expansion workingfluid by condensing transfer system 220 may also be used to enhancebiological nutrient removal processes when the system is deployed at awastewater treatment plant. As one example not limiting upon the scopeof this invention, certain aspects of biological nutrient removalinvolve an aerobic process comprising nitrification of effluent ammoniainto nitrites via one or more first classes of organisms and via one ormore second classes of organisms to convert said nitrites into nitrates.Following the nitrification process, denitrification is performed byexposing the produced nitrates to reaction with heterotrophic bacteriacultures in an anoxic environment to yield nitrogen gas. Thesenitrification and subsequent denitrification processes convert thenitrogen present in effluent ammonia into free nitrogen gas and othernon-effluent byproducts, principally water and gasses includinghydrogen, oxygen, and carbon dioxide. In this manner, biologicalnutrients are removed from the wastewater effluent as a part of theoverall process of water purification and reclamation.

Proper temperature is critical to the nitrification process. Atemperature in the range of 85°-95° F. is preferred to maximize the rateof nitrification, with a reduction of about 18° F. below this levelcausing a decrease in said nitrification rate of approximately 30%. Thislower efficiency would require an increase in the mixed liquor suspendedsolids (MLSS) of the effluent/organism mixture of approximately 300% tomaintain a constant level of nitrification. Such increase is typicallyrequired on a seasonal basis for wastewater treatment plants inlocations where temperatures vary throughout the year, and operators arepresently faced with the unenviable task of determining and adjustingMLSS for proper operation of their facilities. If the temperature of theaerobic nitrification process could be maintained within the desiredrange of 85°-95° F. throughout the year without incurring any additionaloperational cost, such as the consumption of electric power to provideheat for this purpose, a substantial advantage over the present artwould be realized. Consistent operation could be achieved without theneed to adjust MLSS content in bioreactors to compensate for seasonalambient temperature variations as required by present art systems.

In one embodiment of the present invention, one or more secondary heatexchanger(s) 228 may be configured to provide heat from the heatedcondenser heat transfer medium to the nitrification process so as tomaintain the temperature of said process at its optimal rate. In thisembodiment, the one or more valve(s) 222 are configured to adjust theflow of heated condenser heat transfer medium to the nitrificationprocess in any desired portion, said portion determined by theavailability of said heated condenser heat transfer medium consideredalong with the demands of any anaerobic digestion process, demands fromany other heat consuming application of the condensing transfer system220, and the relative priority of all of said applications considered onthe whole. Hydrogen gas is produced as a byproduct of the biologicalnutrient removal process, and in some embodiments, this gas may becaptured and burned, either in a boiler or an internal combustionengine, to produce input heat energy for the ORC process in a manneridentical to that of the anaerobic digestion process described elsewhereherein. Present art systems typically dispose of hydrogen byproducts viaan on-site flare. The capture and re-integration of as many incidentalsources of energy as possible, where such sources are presentlydiscarded by systems known in the art, represents a significantadvantage over said known systems and provides increased energyefficiency and performance.

In one embodiment of the present invention, anaerobic digester heatexchanger 223 may be replaced with a heat exchanger configured toprovide heat energy to the aerobic nitrification component of biologicalnutrient removal process in lieu of the anaerobic digestion process (notshown). As the biological nutrient removal process produces hydrogen gasas described above, said hydrogen gas is suitable for combustion ineither an ICE or a boiler in a manner identical to that employed withbiogas generated via the anaerobic digestion process. Accordingly, thisapplication of residual heat energy removed from the ORC working fluidvia the condensation process contributes to the generation of fuel forconsumption by the source of input heat energy for the ORC via thebiological nutrient removal process just as it does with the anaerobicdigestion process described elsewhere herein.

In one embodiment, heat energy for biological nutrient removal may beextracted directly from the source of heat energy also supplying inputheat to the ORC system as depicted in FIG. 6, FIG. 7, and FIG. 9. Saidheat energy may be in addition to, or in lieu of, heat energy providedby condensing transfer system 220, with the preferred point(s) ofextraction of said heat energy determined at least in part by the amountof heat energy available from either or both sources, heat energyrequirements of this or other processes associated with the system, orbased upon any other criteria or according to any other preferences.

Although the disclosure of this example is directed toward the removalof nitrogen from ammonia, a person of ordinary skill in the art willrecognize that the teaching herein is applicable to any other biologicalnutrient removal process requiring or preferring a consistent operatingtemperature. One or more secondary heat exchanger(s) 228 may beconfigured to provide heat energy from the heated condenser heattransfer medium to any other process that contributes, in whole or inpart, to the removal of biological nutrients or the processing andpurification of wastewater. Similarly, in one embodiment, any co-locatedprocess or system requiring consumption (removal) of heat energy may beconfigured to supply heat energy to the ORC working fluid via one ormore additional heat exchangers in heat transfer communication with saidworking fluid (not shown). Alternatively, in one embodiment, heat energymay be removed from any co-located process or system using componentssimilar or identical to the one or more secondary heat exchanger(s) 228described above. Further, in additional embodiments, processes includingbut not limited to desalination and distillation may benefit from heatenergy extracted from post-expansion ORC working fluid in connectionwith one or more water purification processes.

The advantages of this and other related embodiments of the inventionare considerable. Primarily, mechanical and electric power is generatedfrom the biogas waste product of the anaerobic digestion or otherfuel-generating process. Said power may be consumed locally by thewastewater treatment plant for onsite purposes, including but notlimited to pumping and stirring, thereby reducing or eliminatingconsumption of commercial power as is now practiced. Locally-generatedelectric power may also be applied to the commercial power grid fordistribution to other customers, producing an offset to the cost ofpower consumed whenever the ORC system is offline. A considerableadditional advantage is realized by the reduction or elimination offlares now used to burn biogas generated via the anaerobic digestionprocess. Such flares produce emissions, unsightly visual effects, andpotential hazards that would preferably be eliminated when the biogas isconsumed by one or more boilers to provide input heat energy for an ORCsystem. The liquid cooled radiators utilizing treated effluent for heatconsumption from the post-expansion ORC working fluid are bothconsiderably smaller, less expensive to install and maintain, and moreenvironmentally compatible than their air-cooled counterparts. Theadvantages of using anaerobic digestion, biological nutrient removalsystems, or other co-located processes to consume heat energy from theORC system in lieu of consuming electric power or burning only a portionof the generated biogas in separate boiler(s) to heat the processcultures is described in great detail elsewhere herein. And finally, theflexibility of a system that converts waste material into usefulmechanical or electric power and biogas, which biogas is thenadditionally consumed by the same system to optimally generateadditional mechanical or electric power, provides a high degree ofoperational redundancy not known in the prior art.

In addition to anaerobic digestion systems, any application benefitingfrom significant heat energy may be similarly integrated with an ORCsystem as a heat receiving system with condensation capacity in themanner taught herein. The anaerobic digestion tank(s) function as asingle subsystem providing combined working fluid condensation and theconsumption of heat energy for beneficial use. As with the heating ofanaerobic digestion tank(s), any application in which coupled heatenergy from the primary media may replace the generation of heat energyvia the consumption of electric power will operate with greaterefficiency and economic benefit and may serve as a heat receiving systemwith condensation capacity. Such applications may include but are notlimited to the heating of water in swimming pools, preheating water forboiler systems, space heating, industrial or large scale domestic hotwater systems, combined heat and power systems, and the like. As aresult, these systems will also provide the dual benefit of providingheat energy normally produced by electric power while simultaneouslyeliminating the need for a separate ORC cooling and condensing system inthe present art.

In some embodiments where insufficient cooling and condensationfunctionality may be available from the anaerobic digestion system forproper operation of the ORC, a supplemental or alternate system may berequired if it is desirable to run the ORC. In some embodiments, the ORCmay serve as a primary cooling system for the prime mover(s). Thedescription of this invention is intended to be enabling and not it willbe evident to those skilled in the art that numerous combinations of theembodiments described above may be implemented together as well asseparately, and all such combinations constitute embodiments effectivelydescribed herein.

What is claimed is:
 1. A method of recovering energy from a wastewatertreatment system, the method comprising steps of: A. apportioning aquantity of heat energy among one or more heat consuming waterpurification process(es) using one or more valve(s); B. using at leastsome of said heat energy by at least one of said one or more waterpurification process(es) to produce at least one byproduct suitable togenerate heat by one or more source(s) of heat energy; C. communicatingsome or all of said at least one byproduct to one or more source(s) ofheat energy; D. generating heat energy by said one or more source(s) ofheat energy using said some or all of said at least one byproduct; E.communicating at least a portion of said generated heat energy to aworking fluid; and F. generating mechanical power via expansion of saidworking fluid in a working fluid expander.
 2. The method of claim 1wherein said one or more source(s) of heat energy comprise at least oneof any of a prime mover, an internal combustion engine, a boiler, a fuelcell, and a microturbine.
 3. The method of claim 1 wherein at least oneof said one or more water purification process(es) comprises at leastone of any of an anaerobic digestion process, an aerobic process, abiological nutrient removal processes, and a combustible gas generationprocess.
 4. The method of claim 1 wherein said at least one byproductcomprises at least one of any of a biogas, methane, hydrogen, and aresidual solid effluent.
 5. The method of claim 1 wherein saidmechanical power is communicated to at least one of any of an electricgenerator, a prime mover, a pump, a combustion engine, a fan, a turbine,and a compressor.
 6. The method of claim 1 wherein the steps ofcommunicating heat energy to a working fluid and generating mechanicalpower are performed via an organic Rankine system.
 7. The method ofclaim 1 wherein said quantity of heat energy apportioned among said oneor more heat consuming water purification process(es) comprises at leasta portion of the heat energy generated by said one or more source(s) ofheat energy.
 8. The method of claim 1 further comprising a step ofapportioning at least some of said quantity of heat energy to at leastone radiator.
 9. The method of claim 8 wherein said quantity of heatenergy apportioned among said one or more heat consuming waterpurification process(es) and said at least one radiator comprises atleast a portion of the heat energy generated by said one or moresource(s) of heat energy.
 10. The method of claim 1 wherein saidquantity of heat energy apportioned among said one or more heatconsuming water purification processes comprises heat energy receivedfrom an organic Rankine cycle system.
 11. The method of claim 10 whereinsaid heat energy received from an organic Rankine cycle system iscommunicated via an alternate medium.
 12. The method of claim 11 whereinsaid alternate medium is at least one of any of air, treated aqueouseffluent, and water.
 13. A wastewater treatment heat energy managementmethod comprising steps of: A. using at least one heat consuming waterpurification process to generate at least one byproduct suitable for usein heat generation; B. generating heat energy by consuming saidbyproduct by at least one source of heat energy; C. communicating atleast a portion of said generated heat energy to a working fluid tocreate heated working fluid; D. generating mechanical power by expandingsaid heated working fluid in a working fluid expander; E. apportioningand communicating at least a portion of heat energy remaining in saidexpanded working fluid to said at least one heat consuming waterpurification process using one or more valves; and F. consuming some orall of said communicated expanded working fluid heat energy by said atleast one water purification process.
 14. The method of claim 13 whereinsaid at least one source of heat energy comprises at least one of any ofa prime mover, an internal combustion engine, a boiler, a fuel cell, anda microturbine.
 15. The method of claim 13 wherein said at least onewater purification process comprises at least one of any of an anaerobicdigestion process, an aerobic process, a biological nutrient removalprocesses, and a combustible gas generation process.
 16. The method ofclaim 13 wherein said at least one byproduct comprises at least one ofany of a biogas, methane, hydrogen, and a residual solid effluent. 17.The method of claim 13 wherein said mechanical power is communicated toat least one of any of an electric generator, a prime mover, a pump, acombustion engine, a fan, a turbine, and a compressor.
 18. The method ofclaim 13 wherein the steps of creating heated working fluid andexpanding said heated working fluid in a working fluid expander areperformed using an organic Rankine cycle system.
 19. The method of claim13 wherein the step of apportioning and communicating heat energyfurther comprises a step of apportioning and communicating at least someof said heat energy to at least one radiator.
 20. The method of claim 13wherein said apportioned and communicated heat energy comprises at leasta portion of the heat energy generated by said one or more source(s) ofheat energy.
 21. The method of claim 20 wherein the step of apportioningand communicating heat energy further comprises a step of apportioningand communicating at least some of said heat energy to said at least oneradiator.
 22. The method of claim 13 whereon said quantity of heatenergy apportioned among said one or more heat consuming waterpurification processes comprises heat energy communicated from anorganic Rankine cycle system.
 23. The method of claim 22 wherein saidheat energy communicated from an organic Rankine cycle system iscommunicated via an alternate medium.
 24. The method of claim 23 whereinsaid alternate medium is at least one of any of air, treated aqueouseffluent, and water.